Process for the vapor phase treatment of unsaturated hydrocarbons



March 24,1936. YA. s. .RAMYGE PROCESS FOR THE VAPOR PHASE TREATMENT 0F UNSATLJATED HYDROCARBOS Filed Aug. 2a. 1932 Patented Mar. 24, 1,935y Y* mariani oFFlcE PROCESS FOR THE VAPOR PHASE TREAT- MENT OF UNSATURATED HYDROCAR-- BONS Alexander S. Ramage, Detroit, Mich., assignor to Merlin Wiley and Ora L.,Smitli, trustees, De-

troit, Mich.

Application August 29, 1932, serial No. 630,87?

Claims.

My invention relatesto a new and useful process for the vapor, phase treatment of unsaturated hydrocarbons and particularly to such a press adapted to produce hydrocarbon products having dilering characteristics than the material treated.

As an example of products which may be obtained by the use of a process embodying my invention, I have produced hydrocarbon mixtures composed principally of alcohols and aromatics with other hydroc-arbons in differing proportions, the said mixture having an octane rating which varies from 110 to 138 and an aniline point which varies from zero degrees Fahrenheit to degrees below zero Fahrenheit. Such mixtures may k15 be used for various useful purposes as, for example, a motor fuel spirit or a solvent or extender for paints, lacquers, or the like.

In order better to explain my invention, certain terms will be used throughout the specification which I here define as follows:

Dehydrogenatz'on.-By this term is meant an action in which hydrogen atoms are split 01T the material treated, producing a product relatively poorer in hydrogen than the material treated.

Oxidation-By this term is meant an action in which oxygen is added to the product treated.

Hydrogenation.-,By this term is meant an action in which hydrogen is added to the product treated.

Unsatarated hydrocarbon-As here used, this term includes vapors of all the unsaturated hydrocarbons either of a single group or of a mixture of several groups having thev general formulas CnH2n, CnH2n-2, CnH2n-4 Aromatics--Ashere used, this term relates to a hydrocarbon mixture composed principally of hydrocarbons having the general formula of CnH2ns and including particularly benzol, toluol, xylol, mesitylene and cumcne, with the addition of some naphthenes and olens in the mixture.

A process embodying my invention uses as a starting material the vapors of unsaturated hydrocarbon products included in the term oleni'c vapors. To such vapors varying amounts of carbon dioxide, carbon monoxide, hydrogen and water are added.

In order to facilitate a more ready understanding of the process embodying my invention, I

have shown in Fig. 1 of the -accompanying drawing a. schematic drawing of an apparatus which ma'y be used in a plant designed to operate cna..-

process embodying my invention.. In Fig. 2 of the accompanying drawing, I have shown a chart of various temperatures to be used in carrying 55 out the reactions indicated.

(Cl. 26o-156) Description of apparatus Referring to Fig. 1, 3 designates a still which contains the starting material. The vapors from this material now from the still 3 through a conduit I leading to a metering valve 5. In case -it is desired to add steam to these vapors, it may be admitted through the metering valve 5I. A water gas producer 6 is connected with a conduit Iv terminating in agas reservoir 8. A conduit o 9 connects the gas reservoir 8 with'a compressor l I0, from which a conduit II leads to a metering valve I2. A conduit I3 leads from a source of carbon dioxide under pressure and leads to a metering valve I4. A conduit I5 leads from the 15 metering valve I4 to a pressure reservoir I6. A conduit I'I extends into the pressure reservoir I6 from a metering valve I8, which is connected with a conduit I9. Aconduit 20 leads from the pressure reservoir i5 to ametering valve 2|.

Tubes 22 terminate in a conduit portion which 2 connects with each ofthe metering valves 5, I2

' and 2 I, and permits the passing of gases `from each of said valves to the interior of the tubes 22. The

to a chamber 25 wherein the liquid condensate 301 isseparated from `the gaseous portion of the vapors. Vapors from the chamber 25 pass through a conduit 26 communicating with a compressor y 21. The .compressor 2l drives the 'gases through 36 the conduit 28 to a scrubbing tower 29. Wash oil is introduced into the scrubbing tower 2 9 through a conduit 30, whichextends through the top thereof.

The conduit'30 is operatively connected with a valve.3I, which is connected with a conduit 32 leading to the wash oil pump 33. 'Ihe Wash oil pump 33v is connected with a conduit 34 leading from a wash oil reservoir 35. Charged wash oil from the tower 29 issues from the bottom of the tower 29 to the tank 44, thence-to conduit 45 to pump 46, thence by conduit /41 through heat exchanger 39, and thence to the middle of fractionating tower 42a of wash oil still 42. l The vapors from the still 42 pass from the top of the 50 fractionating tower 42aby conduit 50 through condenser 4I to storage tank 40. The distilled wash oil in still 42 continuously leaves by conduit 43 in counter current through heat exchanger 39, thence through4 conduit 38 to cooler 65 31, thence through conduit 36 to wash oil storage tank 35.

The conduit I9 connects with the scrubbing tower 29 and Kpermits the drawing off of the scrubbed gases which pass through the tower 29l and through the metering valve I8 to the conduit II and to the pressure reservoir I6 for mixing with the carbon dioxide introduced therein when it is desired to recycle the gases through the process. If it is not desired to recycle lthe gases through the process, or if at any time a surplus of gas is -present in the'process, the gases may be Withdrawn from the conduit I9 through a metering valve 48. If it is not desired to recycle any of these gases in the process, the metering valve I8 is closed and the metering valve 48 is opened, and the gases pass through' the conduit 49, which may lead to any desired point.

The operation of my process through the apparatus heretofore described issubstantially as follows: Vapors of the starting material pass from the still 3 through the conduit 4 and through the metering valve 5 at a predetermined and controlled rate and pass into the conduit attached to the tubes 22. At the same time 'water gas is produced in theV water gas producer 6 and passes through the gas reservoir 8 and the compressor I0 to the metering valve I2, through which it is permitted to pass into the conduit of the tubes 22 at a predetermined rate. At the same time, carbon dioxide is metered into the reservoir IS-through the metering valve I4, and if desired, is there mixed with the gases coming from the scrubbing tower `29 which are metered through the valve I8 at a predetermined rate, or may be used without the mixture of the other gases.

The intermixed carbon dioxide and recycled gases or the pure carbon. dioxide then pass through theV conduit 20 and through the metering valve 2l to the conduit attached to the tubes 22. The rate of flow of the carbon dioxide or mixture of carbon dioxide and` scrubbed gas to be recycled is controlled by the metering valve 2| 'I'hus the mixture of gases introduced into the tubes 22 is definitely controlled through the metering valves 5, I2, I4, I8 and 2|. The gases are thus mixed in definite proportions in the tubes 22. 'Ihe tubes 22 contain steel wool, iron turnings, or finely divided reduced iron, which is heated to a. predetermined temperature vary-l ing from 1100 degrees Fahrenheit to 1500 degrees Fahrenheit, depending upon the nature-of the starting material. through the tubes 22 likewise is regulated by the metering valves 5, I2 and 2I and the vapors created in the tubes 22 pass through the condenser 24. 'I'heliquid condensate passes into the reservoir 25 and the gaseous portion of the vapors is passed through the conduit.26 to the compressor 21, from which they are driven into the scrubbing tower 29. There the gases are washed with wash oil coming through the conduit 30. 'I'he wash oil being recycled through The rate of flow of gas Starting material As a starting material for a process embodying my invention, I propose to use the vapors of unsaturated hydrocarbons as heretofore defined.`

Such material may be prepared in any desired manner. For practical purposes I prefer to prepare the material either by the process of my United States Patent No. 1,224,787, in which satited, however, to the Yuse of the starting material produced by either of these processes, but may also be used successfully with unsaturated vapors produced by other methods, such for example as the treatment of alcohols with sulphuric or phosphoric acid, or by heating the alkyl halogen compounds, such as the chlorides, bromides, or iodides, with alcoholic potash, or by the electrolysis of the alkali saltsof dibasic acids.

If the unsaturated hydrocarbon vapors are produced by any of the three last named methods it will be found that the vapors are dry vapors and do not have a suflicient quantity of moisture present to carry out the indicated reactions. If, therefore, such vapors are used, or if the vapors produced by other methods are deficient in the amount of moisture contained therein, sufficient Water in the form of steam should be added through metering valve 5I to the vapors of the starting material to carry out fully the hereinafter indicated reactions.

' The-amount of water required may be ca1cu.

lated by those skilled in the art. The nature of lthe vapor and the method used for producing it must be considered carefully in such calculations. For example, if the-vapors are produced by the method of my United States Patent No. 1,224,787, or by the method of the Strache and Porges United States Patent No. 1,205,578, it will be found that the reactions forming the vapors from a hydrocarbon of the paraffin series will produce by dehydrogenation one molecule of water for each molecule *of olefin formed. This amount of Water is present in the Vapor in the form of steam and must be considered in any computation as to the amount of ,Water required in a process embodying my present invention when vsuch vapors are used asv the starting material.

In producing unsaturated hydrocarbon vapors by the process of my United States Patent No. 1,224,787, I have found that the quantity of water present per one hundred gallons oi oil treated also Varies with the material employed as the starting material. -Examples of this variation may be seen in the followingchart:

. Gallons of Starting Produced Specific water per material material gravity 100 gallons 0I oil CMTJ; CMH 818 6.72 0141130 Culla 770 7. 06 CHU GRH 760 s. 09 01H15 01H14 688 l2. 41 05H14' 06H11 Y 663` 15. 58

In calculating the amount of water required it must be noted also that in practice about 70% only of the hydrocarbon reacts and about 30% of the hydrocarbon becomes converted to gases.

Therefore, .the amount of water required must be calculated on thebasis of' this 70%l which reacts instead of the 100% of 4which 30% is converted to a gas. For this reason it is considered Athan the value of the oil converted to the gas.

The vapors used as the starting material should be nearly or quite free from the presence of saturated hydrocarbons, because if su'ch hydrocarbons are present in any considerable amounts, cracking will result in the tubes and the accompanying deposition of carbon will tend to plug up thc exit tubes. In order, therefore, to insure the substantial absence of any such saturated hydrocarbons. I prefer to pass the vapors used over either ferric or cupric oxide, which may be heated to a, suitable temperature, such as 900 dev grees Fahrenheit.

A Description of process 'I'he chemical reactions which enterA into a proc-I ess embodying myvinvention may occur in any suitable apparatus knownto those skilled in the art. In order, however, to aid in the detailed description of a process embodying my invention, reference will be made to the apparatus shown in the accompanying schematic drawing, which has heretofore been described in detail.

The` vapors employed as the starting material are mixedwith carbon dioxide only or mixtures of carbon dioxide and carbon monoxide, hydrogen and water in varying amounts, depending upon the starting materials and the resultant products desired.

In addition, desirable results also hav; resulted from the recycling of the gases forme-d during the process with the intermixed gases and olefnic vapors. The intel-mixed gases are passed into the entry end of the tubes 22, which are filled with steel wool, iron turnings, or finely divided reduce'd iron, the temperature of these tubes being preferably maintained at a temperature ranging from 1100 degrees Fahrenheit to 1500 degrees Fahrenheit. It is not practical to state any general definite temperatures, as the temperature must be closely regulated according to the naturey of the vapor treated and the length of the tubes and the time of exposures to the reacting material.

In an embodiment of my invention which has been used successfully, I have found that if the tubes 22 are arranged in sets of three, with the lowest temperatures in the entry tube and the -highest temperatures in the exit tube, and with 54 feet of tubing to be traversed by the gases, and with a flow of starting material through 3 inch tubes of 6 to 8 gallons per hour, the temperatures as shown in the chart Fig. 2 may be used advantageously. 1

The reactions involved are complicated an are not .fully known, but are indicated in part at least in the following formulas which represent the actions occurring in the process embodying my invention when various kinds of starting materials are employed, to which are added different kinds of materials in varying amounts tol give varying resultant products. f 1,. 2Ci6H32+2COz+2H20= In all these reactions it will be clearly noticed that the amount of water used is always found practically the saine as that contained in the product and which can be separated and meas ured. However, this same water has undergone many changes, the water primarily used being decomposed by the metallic iron into nascent or active hydrogen, and oxide of iron.

This oxide of iron immediately dehydrogenates the olefin to the lower content of hydrogen liber? ating water. and forming metallic iron." These again combine to oxide and nascent hydrogen, and the oxide again dehydrogenates the unsatu'- rated hydrocarbon until CnHzn-s is formed.

So that the water at first used is consumed and its place is made up by the water formed by def hydrogenation.

The products resulting from the reactions indicated in the above formulas are, in my`opinion, produced as a result of three distinct reactions which occur simultaneously under the conditions stated. These reactions are as follows:

(1) Oxidation, resulting from the use of carf bon dioxide. the presence of metallic iron gives up to one atom of oxygen, leaving carbon monoxide. 'Ihis reaction starts 4at about 600 degrees Fahrenheit and is complete at 1100 degrees Fahrenheit. This may be expressed by way of example by the following formula: C2H4|2CO2=2CH2O+2CO.

(2) Hydrogenation, resulting from the presence of nascent or active hydrogen in the reaction. Probably this hydrogen results from the reaction between the water present andthe metal- Ilic iron, in accordance with formula y 'I'he hydrogen resulting from the reaction is in the nascent or active state and immediately combines with the aldehyde resulting from the oxidation of the hydrocarbon, and forms alcohol, probably in accordance with the following .formulaz 2cHro+2H2=2crI3oH- Y It is known that carbon dioxide in l'ns oxide of iron to metallic iron with the formation of water, which reacts with the heated metallic iron to liberate nascent hydrogen used as the hydrogenating material. This reaction is probably expressed by the following formulas;

It is to be observed that in the dehydrogenation.

molecules of nascent or ac tive hydrogen are, liberated and are available for use as the hydrogenating material as above described. It is to be observed, however, that to complete the hydrogenation heretofore described, six molecules of hydrogen are required.

It is necessary, therefore, to complete the entire hydrogenation above outlined, that two molecules of any olefin employed be dehydrogenated to the aromatic in accordance with the above stated formulas, which will produce six molecules of nascent or active hydrogen. f

A process embodying my invention may be carried on at substantially atmospheric pressures. All of the above stated reactions have been found to occur satisfactorily without the use of pres-- sures substantially above atmospheric pressure.

The foregoing reactions are found to take place in the tubes and should be completed by the time that the vapors emerge from the exit end of the are nally cooled, condensed, and the condensate separated from the condensed water. This condensed water must be distilled to separate the water soluble alcohols which after rectication can be. added to the separated condensate. 'Ihe gas is then scrubbed in any well known apparatus to extract the aromatic and higher olefins, or\the gas can be compressed, cooled and expanded, do-- ing external work, to liquefy the ethylene, propylene and butylene, the balance of the gas remaining being pure methane.

Products produced from the process The liquid condensate which may be produced by a process embodying my invention Will be found to vary in variety and characteristics, according to the specific products and treatment thereof which are subjected to the process used as an embodiment of my invention.

One product which may be produced by such a process consists principally of alcohols up to butyl alcohol, particularly methyl, ethyland prop'yl alcohols and aromatics, with small quantities of naphthenes and undecomposed olefins present in the liquid condensate. Such a product, on distillation to a 450 degreesFahrenheit end point, has been found to have a specific gravity of .865,

an octane number of 130, and an aniline pointof.

tion using dilerent types of starting materialsand subjecting such materials to different treatments as indicated in the foregoing formulas Nos. 1 to '7, inclusive, produce variations in the product resulting therefrom. The variations ln the materials used and the liquids produced -as a result of the reactions indicated by the said formulas will be seen by a consideration of the following compilation showing materials used and 'the characteristics of the liquid produced by the reactions indicated in each of said formulas.

gfxT-: Material used Amount Liquid produced Amount Ol l C H gals l'mmfifq 38% 1 ,Ca'-brglo olii.-.'.) 12e lbs octyl alcohol 49% .Y

Col-bon dloxi( )l; 1027 ou. ft Methyl alcohol.. 13% Water required 6.72 gals Octane number..- -79 Water produced 6.72 gals- I ol fl l c n loo gals Aromatics 40e 2 ofiblilc ciif. 149 los Hopry1olooho1 52-72 0l' Carbon dioxide 1214 cu. ft. Methyl nlcoholj... 8% Water required-.. 7.06 gals Octane number. 85 5 Water produced 7 06 gals Olefn oil C ll 100 gals Aromatics 3517 3 Carbonio :(lcili? 163 lbs lloxyl alcollol 49% or Cal-bon dioxide Methyl alcohol.. )6% Water required- Octane number.

Water produced.

Olefin oil C 1I 100 gals Aromatics 477l 4 carbonio oiiil.) 265 lbs .Hexyl alcohol- 37% or Carbon dioxide- 2127 cu. ft- Methyl alcohol. 16% Ethylene 62.2 lbs.-. 800 cu. it-- Octane number.. 107. 5 Water required-- 12.83 gals..

Water produced 8.09 gals r Water to be added 4.74 gals i 5 Oletln oil C H, 100 gals' Aromatics 537 carbonio ol 332 lbs Methyl alcohol.-- 41172 or Carbon dioxide 2657 cu. ft. Octane number... 136 Ethylene 105 lbs-. 1333 ou. ft Water required-. Water produced--. Watfr to be added--- lrlg? Material used Amount Liquid produced Amount 6 Olef'm oil (Culu) 100 gels Aromatics 497 Carbonio acid 243 lbs Methyl alcohol 51 0 or Carbon dioxide Octane number.-- 138 Ethylene 79 lbs-- Water gas 167 lbs Water required-- Water produced- Water to be added- 7 Olefin oil (Cnlilu) Aromatics 51% Carbonio acid Ethyl alcohol 10% or A Carbon dioxide Methyl alcohol. 39% Ethylene 74.6 lbs.-- Octane number- 137 Propylcne 37.3 lbs Y Butyleue 24.8 lhs Water required Water prndnnerl Watcr to be added 7.95 gals Of the foregoing processes embodying my invention, those expressed by the formulas nurn- -bered 4, 5, 6, and 7 appear to me to be the most The gasesproduced by processes embodying my invention have an approximate average analysis as follows:

Per cent Ethylene Prgpylnne 1u Butyl ene 5 Methane- 5U Required materials Amount Products for sale Amount 4 olefin ou (CHEN) 150 gals Liquid condensate 136 gals.

' Water 4.75 gals om 4400 cu. n. Ethylen Isopropyl alcohol" Butyl alcohol.--" Methane.`

5 Olein oil (CuHu) Carbon dioxide-.- Water- 6 Olen oil (011112) Wate 7 olefin oil (cuna) Carbon.dioxide Water Methane The amount of liquid condensate produced from a process embodying my inventionv depends on the starting material used and has been found to vary from 60% to 70% of the oil treated. Computed on the basis of 100 gallons of oil, the gas produced in auch process varies from 3500 cubic feet to 2600 cubic feet, depending on the per- 'centage of liquid condensate produced in the process, according to Whether more or less gas may be desired. The amount of gas may be regulated by the recycling of the gases formed-and automatically liberating the amount of gas desired through the relief Valve 48.

The liquid condensate may be used for many chemical purposes. Its high octane number characteristics make it.valuable as a blending material to increase the octane rating of low` octane gasolines. It also is valuable as a solvent ated in order to insure complete hydrogenation of the products formed, some small trace of hydrogen may be present in the gases. These gases may be utilized in any desired manner known to those skilled in the art. For example, the ethylene may be removed and used in the usual manner to produce ethyl alcohol, ethylene glycol, ethylene dichloride, chlorethylene, etc. The propylene'and butylene may be used for the production of alcohols, and the methane may be used -ln a gas engine to produce electric current consumed in the process. Y

, The'products produced from the gases may he mixed with the liquid condensate, the alcohols when it is to be used as a motor spirit for blending with 10W octane gasolinas, and the chlorides when the product is to be used as asolvent.

Regulation of the process cate whether -the process is functioning properly and will indicate the necessary regulation of the process to produce the desired product.

.'I'he liquid condensate from the condensers should have a specific gravity varying from 32 to 35 degrees Baume, with an end point of 450 degrees Fahrenheit. All fractions of the stream should be miscible or soluble in denatured alcohol in all proportions. If the specific gravity should be found to run over 35 degrees' Baume, the temperature of the tubes is increased until the specific gravity'of the stream drops below 35 degrees Baume. Likewise, if the specific gravity is below 32 degrees Baume, the temperature of the tubes is lowered until the specific gravity of the stream is restored above 32 degrees Baume.

The gases issuing from the condensers should be practically free from carbon dioxide, hydrogen and carbon monoxide, and should contain among analysis of the issuing gases should disclose appreciable quantities of hydrogen, carbon monoxide or carbon dioxide, thevelocity of the gas 2. That the specific gravity of the stream shall not be less than 32 degrees B aum, nor more than 35 degrees Baume.

3. That the analysis of the issuing gases from the condenser, after scrubbing with oil, shall show *practically no hydrogen, carbon monoxide or carbon dioxide, and shall contain from 35% to 45% of ethylene.

Hydrogenation of aldehydes If the liquid condensate is to be usedl for its high octane characteristics, it isabsolutely essential that all of the aldehydes formed in the oxidation of the hydrocarbon b e completely hydrogenated during the process. It has been found that the octane ratings of the aldehydes are very low, even extending to negative ratings. For example, the octane rating of acetaldehyde is 30.8, and as the carbon atom in the aldehyde increases, the octane rating decreases, until in heptyl aldehyde the octane rating has been found to be a -72.7. It is apparent, therefore, that the presence of even small quantities of the aldehydes affects the octane rating of the liquid oo ndensate in an adverse manner.

If, however, the hydrogenation of the aldehydes to alcohols is complete, a liquid having high octane characteristics will result. A study of the octanecharacteristics of the alcohols reveals the following octane ratings:

CHaOH Octane number 172. C2H5OH v -..Octane number 171. CaHvOH Octane number' 141. C4H9OH Octane number 120. CsHnOH Octane number 115,

CSHHOH Octane number 85. CqHn-,OH Octane number 56. CgHuOH Octane number 32.

. practically all converted into alcohols, and also that no ketones are formed.

Reactions in the tubes As heretofore pointed out in connection with the description of' a process embodying my invention, the reactive material in the tubes is steel wool, iron turnings, or nely divided reduced iron. I believe that the metallic iron acts as a reacting material in the process, rather than as a catalyzer, and that the definite chemical reactions taking place in the tubes utilize the metalliciron *as a denitely reacting material. In the normal use of the tubes in carrying out a process embodying my invention', it will be found that these reactions arc so complete and so nearly balanced that the tubes will be found to be' in substantially their original condition'at all times. If, however, for any reason, the material in the tubes becomes oxidized or contaminated with impurities, it may be renewed by suitable treatment with reducing gases, or thematerial may. be replaced with fresh material.

Summary I am aware thatV heretofore there have been processes utilizing a restricted oxidation of a hydrocarbon for the purpose of forming oxidized fatty acids; and that as a result of such processes small amounts of alcohols and aldehydes were produced and were present in the resulting product. I also am aware that dehydrogenation of hydrocarbons has heretofore` been carried out by the action of oxides of iron and steam on hydrocarbons. I believe, however, that no process has heretofore been proposed in which a definite product of predetermined characteristicsl is produced, by the simultaneous oxidation, hydrogenation, and dehydrogenation of the hydrocarbon employed as va. starting material, particularly where the oxidation resultsfrom the use of an inert oxidizing gas such as carbon dioxide. m

From the foregoing it s apparent that a process embodying my invention consists of separate but simultaneously occurring reactions resulting (1) The decomposition of water present in the reaction by the use of iron maintained at a red heat with the production of iron oxide and the i liberation of active or nascent hydrogen.

(2) The-dehydrogenation of the unsaturated hydrocarbon by the oxide of iron, with the formationof aromatics, water and metallic' iron.

(3) Oxidation by the carbon dioxide acting on the unsaturated hydrocarbon, with the formation of aldehydes and carbon monoxide.

(4) Hydrogenation by the liberated active or -nascent hydrogen acting on the aldehydes to form alcohols, on the carbon monoxide to form alde-f hydes, and on thevaldehydes to form alcohols.

Processes embodying my invention may be varied in order that they may be utilized for the` disclosure hereinto any of the matters of detailV therein stated, but desire to avail myself of all processes included within the scope of the accompanying claims. i ,l

1. A process for the vapor phase treatment of unsaturated hydrocarbons which consists in introducing carbon dioxide in said hydrocarbon vapor and subjecting the resulting vapors to temperatures from 1000 to 1500 F. in the presence of metallic iron and steam, at substantially atmospheric pressures.

2. A process for the vapor phase treatment' of olenic hydrocarbons which consists in admixing steam and carbon dioxide gas with the vapors of oleflnic hydrocarbons and subjecting the resultant admxture to temperatures of from about 1000o F. to about 1500 F. in the presence of metallic iron and steam at substantially atmospheric pressures to effect a dehydrogenation of said hydrocarbons in their vapor phase and to eiect a substantially simultaneous oxidation of the resultant vapor to form aldehydes and oxidized hydrocarbon gases, and thereafter subjecting the aldehydes and other oxidized hydrocarbon gases to substantially simultaneous hydrogenation with nascent hydrogen liberated bythe reactions efiecting th'e dehydrogenation of the said vapors.;

3. A process for the vapor phase treatment of olenic hydrocarbons which consists in admixing earbondioxide with said vapors and subjecting the resultant admixture to temperatures of from about l000 F. to about 1500 F. in the presence of metallic iron and steam at substantially atmospheric pressures, thereby eiecting a dehydrogenation of said hydrocarbons in their vapor phase-'and the substantially simultaneous oxidization of the resultant vapor with the formation of `aldehydes and oxidized hydrocarbon gases, and subjecting the aldehydes and other oxidized hydrocarbon gases to substantially simultaneous hydrogenation by nascent or active hydrogen liberated during the dehydrogenation of the said vapors.

4. A process for the production of aromatics and alcohols from oleiinic hydrocarbon gases and vapors at substantially atmospheric pressure, which consists in admixing carbon dioxide with said oleflnic vapors and gases, and then subject? ing the resultant admixture to temperatures from about I000 F. to about 1500 F. in the presence of metallic iron.

5.v A process for the vapor phase treatment of olenic and other unsaturated hydrocarbons, which consists in the steps of providing a suitable quantity of anunsaturated hydrocarbon vafpor containing ya considerable quantity of oleflnic gases and vapors, admixing carbon dioxide therewith, and thereafter subjecting the resultant ad- SureS.

ALEXANDER s. RAMAGE.- 

